CN101805100B - Method for improving activated sludge concentration in alcohol wastewater full-distillage anaerobic digestion process - Google Patents
Method for improving activated sludge concentration in alcohol wastewater full-distillage anaerobic digestion process Download PDFInfo
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Abstract
The invention relates to a method for improving activated sludge concentration in the alcohol wastewater full-distillage anaerobic digestion process. Corn, wheat, paddy rice, sweet potato, sugar-cane, cassava, sweet sorghum and plant straw containing cellulose from the alcohol production process serve as raw materials; and full-distillage waste mash produced in the alcohol production process is subjected to processes of two-stage anaerobic, aerobic, anaerobic activated sludge separation, anaerobic activated sludge concentration and recovery, liquid solid separation, dry-distillage combustion and advanced wastewater treatment. Primary anaerobic effluent containing sludge exhausted from a primary anaerobic jar is fed to an activated sludge recovery device. In the activated sludge recovery device, the primary anaerobic effluent passes through screening equipment to obtain an undersized material of the activated sludge-enriched primary anaerobic water and a sludge-enriched oversized material; and the COD concentration of secondary anaerobic effluent is below 500mg through the aerobic operation in an aerobic jar. The aerobic jar effluent is fed to an advanced wastewater treatment device, the COD concentration of the sewage subjected to the advanced treatment can be less than 100mg/L, and the sewage is discharged after reaching the standard.
Description
Technical field
The present invention relates to improve alcohol (also claims: the method for wastewater full-distillage anaerobic digestion process activated sludge concentration ethanol); This method adopts two-stage anaerobic, anaerobic activated sludge to concentrate reuse, and technology such as slag mud drying and burning have improved activated sludge concentration in the alcohol wastewater full-distillage anaerobic digestion process; Strengthened anaerobic operation; Improve yield of methane, realized the decrement discharge of anaerobic sludge, solved the sludge moisture content height that present alcohol wastewater full-distillage treatment process exists; Problems such as processing costs height have solved the gordian technique bottleneck of restriction alcohol wastewater full-distillage treatment process realization cleaner production.
Background technology
The bio-ethanol that with biomass is raw material production is a kind of reproducible important foundation raw material and product.The bio-ethanol that with biomass is raw material production is a kind of reproducible important foundation raw material and product.In recent years, along with the development of novel substitute energy fuel ethanol industrial, be raw material production bio-ethanol product with farm crop such as corns merely, can produce the new problem of striving grain with the people.Therefore, in recent years, become bio-ethanol technology trends in the world wide with " non-grain is main " development bio-ethanol, and the emphasis of China's Energy policy and nursery finance.
With starchiness, saccharic and to contain cellulosic straw etc. be raw material production alcohol, production process adopts operating procedures such as the fermentation of band slag, rectifying usually, and the waste water of generation contains the alcohol waste mash of more solid formation.The alcohol waste mash that discharges in the ethanol produce process (also claiming alcohol waste water); Be a kind of high density, high-temperature, high suspended matter, viscosity big, be tart organic waste water; Mainly contain materials such as remaining starch, sugar, crude protein, Mierocrystalline cellulose, various inorganic salt and mycoprotein in the waste water, account for 20～80% of suspended solids content.The exhaust temperature of fresh biological alcohol waste water is 70～100 ℃, and the pH value is 3～5, and COD concentration is 20000～80000mg/L, and biodegradability is stronger, has potential resource characteristic capable of using.
Traditional alcohol wastewater full-distillage anaerobic technique is at first sent into anaerobic jar and is carried out anaerobic treatment for containing solid full lees wastewater, and the solid anaerobism water that contains after the processing is delivered to liquid-solid separation device slag mud is removed; Active anaerobic sludges a large amount of in the anaerobic jar are discharged with slag mud; Make the active sludge storage in the anaerobic jar lower, cause full lees wastewater anaerobic operation unstable, anaerobic digestion is unusual; Yield of methane is low, and ton alcohol biogas output has only 150Nm usually
3, the anaerobism water viscosity of discharging is big simultaneously, liquid-solid separation difficulty, and COD is higher, and full lees wastewater anaerobic operation volumetric loading is usually at 2.5kgCOD/m
3.d about, alcohol cleaner production and economic benefit have been influenced.
Alcohol waste water is handled and to be adopted full-distillage anaerobic digestion to handle with liquid-solid traditionally usually to separate two kinds of technologies; Full-distillage anaerobic digestion is handled and is directly adopted full-distillage anaerobic digestion to handle to the useless mash that contains more solid formation; Be that alcohol waste mash does not carry out liquid-solid separating treatment; And alcohol residue liquid-liquid-solid separating technology carries out liquid-solid separating treatment earlier to useless mash, reclaims the solid phase product again, handles clear liquid.For Mierocrystalline celluloses such as, sweet sorghum and stalks is the useless mash that produces behind the raw material production alcohol; Its solid phase added value of product is low; Adopt the useless liquid-solid separating treatment process economics of mash of poor benefits; Advantages such as employing full-distillage anaerobic digestion treatment process has the biogas output height usually, and economic benefit is high, sludge discharge is few.But; Alcohol waste mash adopts traditional full-distillage anaerobic digestion to handle and exists the plant investment height, anaerobic operation efficient is low; Fluctuation of service, the sludge treatment difficulty, COD exceeds standard in the discharge of wastewater; And unstable, this problem is perplexing full-distillage anaerobic digestion treatment process applying in ethanol produce enterprise always.
Summary of the invention
In order to solve the problem that traditional alcohol wastewater full-distillage anaerobic digestion treatment process exists, the present invention proposes a kind of method that improves activated sludge concentration in alcohol wastewater full-distillage anaerobic digestion process, its technical scheme and characteristic are following:
From the ethanol produce process with corn, wheat, paddy rice, Ipomoea batatas, sugarcane, cassava, sweet sorghum and to contain cellulosic straw be raw material; Produce the complete poor useless mash that the alcohol process produces, through two-stage anaerobic, aerobic, anaerobic activated sludge separates, anaerobic activated sludge concentrates reuse, anaerobic activated sludge reuse, liquid-solid separation, do poor burning and waste water advanced treating processes; Active sludge tripping device 8 is delivered in an anaerobism water outlet that contains slag mud of anaerobic jar 1 discharging; In active sludge tripping device 8, the water outlet of one-level anaerobism water obtain through screening plant the enrichment active sludge one-level anaerobism water screen underflow and be rich in the screen overflow of slag mud.
The sieve diameter of the screening plant of said active sludge tripping device 8 is 0.05～1 millimeter, and the recovery of controlling active sludge through adjustment sieve diameter and screening residence time of material is 40～95%.
The concentrated active sludge that sludge settling concentrating unit 7 obtains returns one-level anaerobic jar 1; Keep the higher activated sludge concentration of one-level anaerobic jar 1; The volumetric loading that makes waste water one-level anaerobic operation is greater than 7.0kgCOD/m3d, and the active sludge natural pond part of returning has been increased biogas output by anaerobic digestion.
The COD concentration of useless mash is 20000～80000mg/L, and the COD of sewage concentration after the advanced treatment is less than 100mg/L.
A kind of idiographic flow of the method that improves activated sludge concentration in alcohol wastewater full-distillage anaerobic digestion process is referring to accompanying drawing, a kind of method flow diagram that improves activated sludge concentration in alcohol wastewater full-distillage anaerobic digestion process, and operating process specifies as follows:
COD concentration from the ethanol produce process is the full lees wastewater of 20000～80000mg/L; Deliver to one-level anaerobic jar 1; One-level anaerobic jar 1 is provided with interchanger, the service temperature of control one-level anaerobic jar 1, and an anaerobic jar 1 is complete hybrid high temperature anaerobic reactor drum; The anaerobic operation temperature is controlled to be 55～65 ℃, and the volumetric loading of full lees wastewater anaerobic operation reaches more than the 7.0kgCOD/m3.d.Waste water is after an anaerobic treatment; Obtain COD less than the water outlet of 7000mg/L one-level anaerobism water; The biogas that the one-level anaerobic operation produces is delivered to the biogas storage tank; Biogas output and traditional technology have relatively improved more than 20%, and methane purity is that active sludge tripping device 8 is delivered in the anaerobism water outlet that contains a large amount of slag mud of 50～65%, anaerobic jar, 1 discharging in the biogas.
In active sludge tripping device 8; One-level anaerobism water water outlet from an anaerobic jar 1; Obtain through screening plant the enrichment active sludge one-level anaerobism water screen underflow and be rich in the screen overflow of slag mud; The sieve diameter of screening plant is 0.05～1 millimeter, and it is 40～95% that the variation of sieve diameter and screening residence time of material makes the recovery control bit of active sludge.The one-level anaerobism water of enrichment active sludge is delivered to sludge settling concentrating unit 7; Obtain spissated active sludge through sludge settling concentrating unit 7 precipitation operation; In the one-level anaerobism water of enrichment active sludge; Can further digest the organic solid granule of being rich in of degraded owing to also contain simultaneously, also return one-level anaerobic jar 1 and carry out digestion process again, increase biogas output with concentrated active sludge; Higher activated sludge concentration, the volumetric loading that makes waste water one-level anaerobic operation is greater than 7.0kgCOD/m3d; Screen overflow slag mud is delivered to liquid-solid separating centrifuge 2, and further dehydration is concentrated with slag mud through liquid-solid separating centrifuge 2, and isolated liquid phase is delivered to secondary anaerobic jar 4, and the slag mud solid phase water cut after the dehydration is 60～75%.Slag mud after the dehydration continues to deliver to slag mud drying installation 3 dryings, and the poor fuel as drying installation 3 of doing that obtains after the oven dry uses.
Secondary anaerobic jar 4 is provided with the waste water cooling tower; The service temperature of control secondary anaerobic jar 4 is 33～38 ℃; Regularly the anaerobic sludge of discharging is also delivered to one-level anaerobic jar 1; Enhanced primary anaerobic operation, the effluent COD concentration of secondary anaerobic water are below the 1500mg/L, and deliver to aerobic jar 5 aerobic treatment of carrying out bubbling air.
Secondary anaerobic water is through the aerobic operation in aerobic jar 5, and making water outlet get COD concentration is below the 500mg/L.Waste water advanced treatment unit 6 is delivered in aerobic jar of water outlet, through adding oxygenants such as ozone aerobic water is carried out further deep oxidation processing, and the COD of sewage concentration after the advanced treatment can realize the sewage qualified discharge less than 100mg/L.
A kind of method that improves activated sludge concentration in alcohol wastewater full-distillage anaerobic digestion process that the present invention relates to; This method adopts two-stage anaerobic, anaerobic activated sludge to concentrate technology such as reuse, has strengthened anaerobic operation, has reduced the COD content in investment and the waste discharge; Improved yield of methane; Realized the decrement discharge of anaerobic sludge, solved the gordian technique bottleneck of restriction ethanol produce realization cleaner production, economic and social benefit is obvious.
Description of drawings
Figure is a kind of method flow diagram that improves activated sludge concentration in alcohol wastewater full-distillage anaerobic digestion process.
1 is the one-level anaerobic jar among the figure, and 2 is liquid-solid separating centrifuge, and 3 is slag mud drying installation, and 4 is the secondary anaerobic jar, and 5 is aerobic jar, and 6 is waste water advanced treatment unit, and 7 is the sludge settling concentrating unit, and 8 is the active sludge tripping device
Embodiment
Below in conjunction with accompanying drawing the present invention is done further detailed description:
The alcohol waste water that produces in the corn straw ethanol produce process adopts method shown in Figure 1 to handle; From the ethanol produce process with corn, wheat, paddy rice, Ipomoea batatas, sugarcane, cassava, sweet sorghum and to contain cellulosic straw be raw material; Produce the complete poor useless mash that the alcohol process produces, through two-stage anaerobic, aerobic, anaerobic activated sludge separates, anaerobic activated sludge concentrates reuse, anaerobic activated sludge reuse, liquid-solid separation, do poor burning and waste water advanced treating processes; Active sludge tripping device 8 is delivered in an anaerobism water outlet that contains slag mud of anaerobic jar 1 discharging; In active sludge tripping device 8, the water outlet of one-level anaerobism water obtain through screening plant the enrichment active sludge one-level anaerobism water screen underflow and be rich in the screen overflow of slag mud.The sieve diameter of the screening plant of active sludge tripping device 8 is 0.05～1 millimeter, and the recovery of controlling active sludge through adjustment sieve diameter and screening residence time of material is 40～95%.The concentrated active sludge that sludge settling concentrating unit 7 obtains returns one-level anaerobic jar 1; Keep the higher activated sludge concentration of one-level anaerobic jar 1; The volumetric loading that makes waste water one-level anaerobic operation is greater than 7.0kgCOD/m3d, and the active sludge natural pond part of returning has been increased biogas output by anaerobic digestion.
The COD concentration of useless mash is 20000～80000mg/L, and the COD of sewage concentration after the advanced treatment is less than 100mg/L.
Embodiment:
COD concentration from corn straw ethanol produce process is the waste water of 60000mg/L; Deliver to one-level anaerobic jar 1; One-level anaerobic jar 1 is provided with interchanger; The service temperature of control one-level anaerobic jar 1 is 60 ℃, and an anaerobic jar 1 is complete hybrid high temperature anaerobic reactor drum, and the volumetric loading of anaerobic waste water operation reaches 8.0kgCOD/m3.d.Waste water is after an anaerobic treatment; Obtain COD less than the water outlet of 6000mg/L one-level anaerobism water; The biogas that the one-level anaerobic operation produces is delivered to the biogas storage tank, and methane purity is 55% in the biogas, and the active sludge natural pond part of returning is by anaerobic digestion; Increased biogas output, active sludge tripping device 8 is delivered in an anaerobism water outlet that contains a large amount of slag mud of anaerobic jar 1 discharging.
In active sludge tripping device 8; Obtain through screening plant from the one-level anaerobism water water outlet of an anaerobic jar 1 the enrichment active sludge one-level anaerobism water screen underflow and be rich in the screen overflow of slag mud; The sieve diameter of screening plant is 0.2 millimeter, and it is 85% that the variation of sieve diameter and screening residence time of material makes the recovery control bit of active sludge.The one-level anaerobism water of enrichment active sludge is delivered to sludge settling concentrating unit 7; Obtain spissated active sludge through sludge settling concentrating unit 7 precipitation operation; Concentrated active sludge turns back to one-level anaerobic jar 1 and carries out digestion process again; Increased biogas output, the volumetric loading of waste water one-level anaerobic operation reaches 8.0kgCOD/m3d; Screen overflow slag mud is delivered to liquid-solid separating centrifuge 2, and further dehydration is concentrated with slag mud through liquid-solid separating centrifuge 2, and isolated liquid phase is delivered to secondary anaerobic jar 4, and the slag mud solid phase water cut after the dehydration is 65%.Slag mud after the dehydration continues to deliver to slag mud drying installation 3 dryings, and the poor fuel as drying installation 3 of doing that obtains after the oven dry uses.
Secondary anaerobic jar 4 is provided with the waste water cooling tower; The service temperature of control secondary anaerobic jar 4 is 34 ℃; Regularly the anaerobic sludge of discharging is also delivered to one-level anaerobic jar 1; The enhanced primary anaerobic operation, the effluent COD concentration of secondary anaerobic water is 800mg/L, and delivers to aerobic jar 5 aerobic treatment of carrying out bubbling air.
Secondary anaerobic water is through the aerobic operation in aerobic jar 5, and making water outlet get COD concentration is below the 300mg/L.Waste water advanced treatment unit 6 is delivered in aerobic jar of water outlet, through adding oxygenants such as ozone aerobic water is carried out further deep oxidation processing, and the COD of sewage concentration after the advanced treatment can realize the sewage qualified discharge less than 100mg/L.
Claims (3)
1. method that improves activated sludge concentration in alcohol wastewater full-distillage anaerobic digestion process; It is characterized in that from the ethanol produce process with corn, wheat, paddy rice, Ipomoea batatas, sugarcane, cassava, sweet sorghum and to contain cellulosic straw be raw material, produce the complete poor useless mash that the alcohol process produces; COD concentration from the ethanol produce process is the complete poor useless mash of 20000～80000mg/L; Deliver to one-level anaerobic jar (1); One-level anaerobic jar (1) is provided with interchanger, the service temperature of control one-level anaerobic jar (1), and one-level anaerobic jar (1) is complete hybrid high temperature anaerobic reactor drum; The anaerobic operation temperature is controlled to be 55～65 ℃, and the volumetric loading of full lees wastewater anaerobic operation reaches 7.0kgCOD/m
3More than the d; Waste water obtains COD less than the water outlet of 7000mg/L one-level anaerobism after the one-level anaerobic treatment; The biogas that the one-level anaerobic operation produces is delivered to the biogas storage tank; Biogas output and traditional technology have relatively improved more than 20%; Methane purity is 50～65% in the biogas, and active sludge tripping device (8) is delivered in the one-level anaerobism water outlet that contains a large amount of slag mud of one-level anaerobic jar (1) discharging; In active sludge tripping device (8); One-level anaerobism water outlet from one-level anaerobic jar (1); Obtain through screening plant the enrichment active sludge the water outlet of one-level anaerobism screen underflow and be rich in the screen overflow of slag mud; The sieve diameter of screening plant is 0.05～1 millimeter, and the variation of sieve diameter and screening residence time of material makes the recovery of active sludge be controlled to be 40～95%; Sludge settling concentrating unit (7) is delivered in the one-level anaerobism water outlet of enrichment active sludge; Obtain spissated active sludge through sludge settling concentrating unit (7) precipitation operation; In the one-level anaerobism water outlet of enrichment active sludge; Can further digest the organic solid granule of being rich in of degraded owing to also contain simultaneously, also return one-level anaerobic jar (1) and carry out digestion process again, increase biogas output with concentrated active sludge; Higher activated sludge concentration, the volumetric loading that makes waste water one-level anaerobic operation is greater than 7.0kgCOD/m
3D; Screen overflow slag mud is delivered to liquid-solid separating centrifuge (2); Further dehydration is concentrated with slag mud through liquid-solid separating centrifuge (2); Isolated liquid phase is delivered to secondary anaerobic jar (4); Slag mud solid phase water cut after the dehydration is 60～75%, and the slag mud after the dehydration continues to deliver to slag mud drying installation (3) drying, and the poor fuel as slag mud drying installation (3) of doing that obtains after the oven dry uses; Secondary anaerobic jar (4) is provided with the waste water cooling tower; The service temperature of control secondary anaerobic jar (4) is 33～38 ℃; Regularly the anaerobic sludge of discharging is also delivered to one-level anaerobic jar (1); Enhanced primary anaerobic operation, the effluent COD concentration of secondary anaerobic water are below the 1500mg/L, and deliver to the aerobic treatment that bubbling air is carried out in aerobic jar (5); The water outlet of secondary anaerobic water is through the aerobic operation in aerobic jar (5); Making effluent COD concentration is below the 500mg/L; Waste water advanced treatment unit (6) is delivered in aerobic jar of water outlet; Through adding the ozone oxidation agent aerobic water is carried out further deep oxidation processing, the COD of sewage concentration after the advanced treatment realizes the sewage qualified discharge less than 100mg/L.
2. the method for claim 1; It is characterized in that sludge settling concentrates the concentrated active sludge that adopts sludge settling concentrating unit (7) to obtain and returns one-level anaerobic jar (1); Keep the activated sludge concentration of one-level anaerobic jar, the volumetric loading that makes waste water one-level anaerobic operation is greater than 7.0kgCOD/m
3D, the active sludge that returns part has been increased biogas output by anaerobic digestion.
3. the method for claim 1 is characterized in that the COD concentration of described useless mash is 20000～80000mg/L, and the COD of sewage concentration after the advanced treatment is less than 100mg/L.
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| CN103102011B (en) * | 2011-11-10 | 2014-05-21 | 中国石油化工股份有限公司 | Anaerobic bio-enhancement treatment method for cellulose ethanol wastewater |
| CN102605003B (en) * | 2012-03-22 | 2013-07-17 | 天津大学 | Method for producing alcohol from potato raw materials |
| CN102874989B (en) * | 2012-10-25 | 2014-10-01 | 宁夏宝塔石化集团有限公司 | Anaerobic and aerobic wastewater treatment method and equipment for recycling high-concentration active sludge |
| CN103266135B (en) * | 2013-04-11 | 2015-01-14 | 清华大学 | Integrated utilization method of banana stalk |
| CN103387313A (en) * | 2013-07-19 | 2013-11-13 | 济南圣泉集团股份有限公司 | Method for treating cellulosic ethanol waste water |
| CN105174601B (en) * | 2015-07-16 | 2017-08-25 | 华南理工大学 | A kind of biological treatment of cassava alcohol waste water |
| WO2018136019A1 (en) | 2017-01-20 | 2018-07-26 | Istanbul Teknik Universitesi | Method for increasing methane yield in anaerobic digesters by the addition ofa cellulolytic bacteria cocktail (cebac-m) developed from a sample taken from an anaerobic reactor acclimated to sorghum |
| CN107055770A (en) * | 2017-05-08 | 2017-08-18 | 中溶科技股份有限公司 | The method of continuous full-mixing type anaerobic reaction treatment high concentration cassava alcohol waste water |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4735724A (en) * | 1986-07-30 | 1988-04-05 | Gas Research Institute | Solids concentrating anaerobic digestion process and apparatus |
| CN1133209A (en) * | 1995-07-28 | 1996-10-16 | 王天光 | Treating process for waste undecanted wine of alcohol |
| CN1271692A (en) * | 1999-04-28 | 2000-11-01 | 辽宁中绿环境工程有限公司 | Process for treating high-concentration sewage |
| CN1778713A (en) * | 2004-11-19 | 2006-05-31 | 刘新萍 | Sewage treatment |
| CN101280322A (en) * | 2008-04-21 | 2008-10-08 | 云浮市九方农业科技发展有限公司 | Anaerobic fermentation method and device of alcohol waste Liquid |
-
2010
- 2010-05-11 CN CN2010101675133A patent/CN101805100B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4735724A (en) * | 1986-07-30 | 1988-04-05 | Gas Research Institute | Solids concentrating anaerobic digestion process and apparatus |
| CN1133209A (en) * | 1995-07-28 | 1996-10-16 | 王天光 | Treating process for waste undecanted wine of alcohol |
| CN1271692A (en) * | 1999-04-28 | 2000-11-01 | 辽宁中绿环境工程有限公司 | Process for treating high-concentration sewage |
| CN1778713A (en) * | 2004-11-19 | 2006-05-31 | 刘新萍 | Sewage treatment |
| CN101280322A (en) * | 2008-04-21 | 2008-10-08 | 云浮市九方农业科技发展有限公司 | Anaerobic fermentation method and device of alcohol waste Liquid |
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